Uop Lcc

Cora Wang Ploentham

Gregory A Funk

Alan K Bedell

Stanley Joseph Frey

Keith Allen Couch

Ram Ganesh Rokkam

David M Banks

Stanley S Carp

Deng-Yang Jan

Stephen W Sohn

Charles P Luebke

Mark Paul Lapinski

Hari S Bajpai

Pelin Cox

Lin Jin

Xi Zhao

Nikunj Manubhai Patel

Vaibhav Ramesh Thool

A process for converting naphtha to light olefins comprises contacting a naphtha stream with a zeolitic catalyst to produce a light paraffin stream. The light paraffin may be separated into an ethane stream and a propane stream. The ethane in the ethane stream may be converted into ethylene, and the propane in the propane in the propane stream may be converted into propylene. The light paraffin stream may also be separated into a heavy stream which may be recycled back to the contacting step.

Process for converting naphtha to light olefins with separation

A process increases the concentration of normal paraffins in a feed stream comprising separating a naphtha feed stream into a normal paraffin rich stream and a non-normal paraffin rich stream. A naphtha feed stream may be separated into a normal paraffin stream and a non-normal paraffin stream. An isomerization feed stream is taken from the non-normal paraffin stream and isomerized over an isomerization catalyst to convert non-normal paraffins to normal paraffins and produce an isomerization effluent stream. The isomerization effluent stream may be separated into a propane stream and a C4+ hydrocarbon stream optionally in a single column. The C4+ hydrocarbon stream may be recycled to the step of separating a naphtha feed stream.

Process for increasing the concentration of normal paraffins in a light naphtha stream

A process for producing light olefins comprising thermal cracking. Hydrocracked streams are thermally cracked in a steam cracker to produce light olefins. A pyrolysis gas stream is separated into a light stream and a heavy stream. A light stream is separated into an aromatic naphtha stream and a non-aromatic naphtha stream. The aromatics can be saturated and thermally cracked. The integrated process may be employed to obtain olefin products of high value from a crude stream.

Integrated process for the conversion of crude to olefins

A process for producing light olefins comprising thermal cracking. Hydrocracked streams are thermally cracked to produce light olefins. A pyrolysis gas stream is separated into a light pyrolysis gas stream and a heavy pyrolysis gas stream. A light pyrolysis gas stream is separated into a normal paraffins stream and a non-normal paraffins stream. A normal paraffins stream is thermally cracked. The integrated process may be employed to obtain olefin products of high value from a crude stream.

A process for increase conversion and yield and selectivity to normal paraffins by reducing the hydrogen to hydrocarbon ratio for paraffin feeds with substantial butanes. The process works best with a low concentration of heavies and cyclics in the isomerization feed. High normal ratios of equilibrium, isobutane conversion, normal paraffins yield and selectivities are achieved for naphtha feed at low ratios of hydrogen to hydrocarbons.

Process for isomerizing isobutane

A process increases the concentration of normal paraffins in a feed stream comprising separating a naphtha feed stream into a normal paraffin rich stream and a non-normal paraffin rich stream. A naphtha feed stream may be separated into a normal paraffin stream and a non-normal paraffin stream. An isomerization feed stream may be taken from the non-normal paraffin stream and isomerized over an isomerization catalyst to convert non-normal paraffins to normal paraffins and produce an isomerization effluent stream. The isomerization effluent stream may be separated into a propane stream and a C4+ hydrocarbon stream optionally in a single column. The C4+ hydrocarbon stream may be recycled to the step of separating a naphtha feed stream.

Process for increasing the concentration of normal hydrocarbons in a light naphtha stream

Improved processes for production of gasoline with 95 RONC including a C-Cisomerization zone, two Cisomerization zones, and a reforming zone are described. The first and second Cisomerization zones share a common stabilizer which strips off the chlorides and removes the light ends. The capital and operating costs of the processes are reduced through the elimination of one of the stabilizer columns and the associated condenser, receiver, trim cooler, and reboiler. The processes improve the RONC of the Cisomerization product because unconverted methylcyclohexane is recycled back to the second Cisomerization zone to be converted into dimethylcyclopentane.

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Elk Grove Village, IL, United States of America

Cora Wang Ploentham